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INTEGRATED LABORATORY SCALE DEMONSTRATION EXPERIMENT OF THE HYBRID SULPHUR CYCLE AND PRELIMINARY SCALE-UP Figure 2: Hybrid sulphur flow sheet (top Section I, bottom Section II) O 2 121e C101 T101a T101b T101c C102 SO 2 + O 2 from section II 105b 103b H 2 O from section II H 2 O 121b E104 123 124 121a 121c 121d 114b E105 114a 114c 112b E106 115a 116a 116b P103 115d E110 115e 101 103a E102 105c 122 D101 113 H 2 SO 4 to section II 112a H 2 120 E101 105a 103c 111a 109 118 102a E103 P101 104 102b P102 106a 106b 111c E109 111b 107a E108 R101 + - 110 107b 108 P104 119 117 Water SO 2 + O 2 To section I A1a H 2 SO 4 from section I A1 A8 A11 KO-201 A2 A9 HX-205 A20 A21 HX-201 A10 VP201 HX-211 A4c A11a HX-212 HX-206 A7b A7a HX-201 8 HX-203 7 HX-202 6 Water HX-208 2c He 3 41 41 40 40 HX-209 E209 HX-203 A20a A21a A3 HX-202 A4b He HX-204 A7 A5a A6 A5 HX-210 2 5a HX-205 5 2b HX-207 43 43 42 42 4 4 -C A3a A4 A4a P201 1 1a P202 P203 2a Section II of the HyS process involves two main steps. The first one concerns H 2 SO 4 concentration to decrease the amount of water which enters the second step with decomposition reactors. The goal of this step is to concentrate sulphuric acid with minimum external heat requirement. The pressure of the liquid mixture of about 52 wt.% H 2 SO 4 , coming from Section I is first dropped adiabatically from 0.2 to 0.1 bar allowing residual SO 2 and O 2 to be removed in knockout drum via gaseous stream, along with some water (KO-201). Next, the liquid stream (52.6 wt.% H 2 SO 4 ) is heated by interchange in a three-heat-exchanger network (HX-201, HX-203, HX-202). The different distilled vapour streams are removed, cooled and condensed at 298 K (HX-211). The residual liquid stream (73.5 wt.% H 2 SO 4 ) is fed into the second vaporisation stage at an operating pressure of 1.5 bar (P201). The stream is first heated by interchange in two heat exchangers (HX-204, HX-205) then in a third exchanger powered by hot stream of helium from the primary heat source (HX-206). The composition of the final stream is controlled by means of a condenser which allows the liquid temperature to be regulated. The chosen parameters are a temperature of 493 K and a pressure of 1.5 bar. With this set of parameters the composition of the liquid phase entering the decomposition step is close to 80 wt.% H 2 SO 4 . 216 NUCLEAR PRODUCTION OF HYDROGEN – © OECD/NEA 2010
INTEGRATED LABORATORY SCALE DEMONSTRATION EXPERIMENT OF THE HYBRID SULPHUR CYCLE AND PRELIMINARY SCALE-UP At the entry of the decomposition step, volumetric pump raises the pressure to the operating value (5 bar) (P-202). The liquid stream is fed to the top of SO 3 recombination reactor (HX-210). This reactor consists of an adiabatic seven-equilibrium stage vapour-liquid contactor device. It operates at the equilibrium pressure of the process with an assumed negligible pressure drop. The goal of this device is to countercurrently wash the gases coming from the decomposer (HX-209) which contains a hot mixture of O 2 , SO 2 , H 2 O and unreacted SO 3 . The gaseous stream is cooled by contact with the liquid sulphuric phase, then SO 3 is converted to H 2 SO 4 in the presence of gaseous water. H 2 SO 4 in the gaseous stream condenses in contact with the cold aqueous sulphuric stream. Concentrated liquid sulphur acid at about 88 wt.% H 2 SO 4 coming from the bottom of reactor at 580 K is sent to the decomposition reactor. The goal is to achieve an equilibrium pressure of 5 bar at the end of the decomposition reactor. The mixture temperature is raised to about 873 K where H 2 SO 4 decomposes almost completely to SO 3 and H 2 O. Next, the gaseous stream enters a set of catalytic reactors in which the SO 3 to SO 2 decomposition reaction takes place (HX-209). The outlet equilibrium temperature and pressure are controlled at 1 123 K and 5 bar. The heat required for decomposition reactors is supplied by a hot stream of helium from the primary heat source. The gaseous stream is cooled in two heat exchangers which allow for heat recovery. The pinch temperature in the interchange heat exchanger is no less than 50 K and the function of the following heat exchanger is to cool the stream to its dew point to avoid condensation. This procedure prevents water dilution of the feed entering the decomposition step. The cooled gaseous mixture is fed to the bottom of recombination reactor, as described earlier. The gaseous mixture leaving the reactor contains mainly SO 2 , O 2 and H 2 O. The outlet temperature is controlled to satisfy the material balance of the cycle by means of partial condenser (HX-202). Flow sheet energy requirements and thermal efficiency The standard formation enthalpy for water is equal to 286 kJ/mole H 2 relative to the formation of liquid water and corresponding to (HHV) of H 2 . The theoretical voltage for pure water decomposition is 1.23 V. However, the majority of conventional electrolysis devices need at least 2.0 V when economically reasonable current densities are maintained. This value translates into a water electrolysis Faraday’s efficiency of about 74%. If a thermal-to-electric conversion efficiency of 45% is assumed, the total equivalent heat requirement corresponds to a heat input of 859 kJ/mole H 2 . In the proposed flow sheet, a high temperature heat input is required in only three locations: the vaporiser and decomposer of H 2 SO 4 (HX-208), the SO 3 catalytic decomposer (HX-209) and the last heat exchanger of concentration step (HX-206). A total of 413.3 kJ/mole H 2 is supplied by the primary heat source. A grand total of 243 kJ/mole H 2 waste heat is rejected to cooling water. Unfortunately the temperature is too low to allow any use of this heat. A total of 120 kJ/mole H 2 electric energy is used in the flow sheet. Nearly 97% of the electric energy is required in Section I with the greatest part for the electrolysis cell. If a thermal-to-electric conversion efficiency of 45% is assumed, the total electric power requirement corresponds to a heat input of 266.7 kJ/mole H 2 . The proposed flow sheet produces hydrogen at a pressure of 10 bar according to the chosen pressure of the electrolysis cell. Compared to the electrolysis of water, whose pressure of hydrogen product is about 1 bar, the power requirement to raise the pressure up to 10 bar is not negligible. The electric power requirement to do such work is about 9.8 kJ/mole H 2 . With this output condition, the new heat requirement for VHTR-powered water electrolysis becomes 881 kJ/mole H 2 With a total equivalent heat requirement of 680 kJ/mole H 2 , the proposed HyS process flow sheet compares favourably to VHTR-powered water electrolysis. Capital assessment method When studying several hydrogen production processes, it can be important to assess the production cost by means of capital, operational and energy costs. The method of capital cost assessment can be selected according to different criteria. These criteria are: current stage of development, innovation level, available time and assessment cost, wished accuracy. First, the choice of the method is based upon the current stage of development. An estimate of the capital expenditures may consist of a pre-design estimate with few process data or a detailed estimate based upon complete drawings and NUCLEAR PRODUCTION OF HYDROGEN – © OECD/NEA 2010 217
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Nuclear Science 2010 Nuclear Produc
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ORGANISATION FOR ECONOMIC CO-OPERAT
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TABLE OF CONTENTS Table of contents
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TABLE OF CONTENTS Y. Gong, E. Chalk
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EXECUTIVE SUMMARY Executive summary
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EXECUTIVE SUMMARY steam turbine, in
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EXECUTIVE SUMMARY sulphur depositio
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EXECUTIVE SUMMARY affords saving 35
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EXECUTIVE SUMMARY safety assessment
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EXECUTIVE SUMMARY The question was
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CHANGING THE WORLD WITH HYDROGEN AN
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NUCLEAR HYDROGEN PRODUCTION PROGRAM
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NUCLEAR HYDROGEN PRODUCTION PROGRAM
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FRENCH RESEARCH STRATEGY TO USE NUC
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PRESENT STATUS OF HTGR AND HYDROGEN
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STATUS OF THE KOREAN NUCLEAR HYDROG
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THE CONCEPT OF NUCLEAR HYDROGEN PRO
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CANADIAN NUCLEAR HYDROGEN R&D PROGR
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APPLICATION OF NUCLEAR-PRODUCED HYD
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STATUS OF THE INL HIGH-TEMPERATURE
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HIGH-TEMPERATURE STEAM ELECTROLYSIS
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MATERIALS DEVELOPMENT FOR SOEC Mate
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A METALLIC SEAL FOR HIGH-TEMPERATUR
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DEGRADATION MECHANISMS IN SOLID OXI
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CAUSES OF DEGRADATION IN A SOLID OX
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70 μm CAUSES OF DEGRADATION IN A S
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NUCLEAR HYDROGEN USING HIGH TEMPERA
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Page 167: SESSION III: THERMOCHEMICAL SULPHUR
Page 170 and 171: CEA ASSESSMENT OF THE SULPHUR-IODIN
Page 181: STATUS OF THE INERI SULPHUR-IODINE
Page 184 and 185: INFLUENCE OF HTR CORE INLET AND OUT
Page 194 and 195: EXPERIMENTAL STUDY OF THE VAPOUR-LI
Page 203: DEVELOPMENT OF HI DECOMPOSITION PRO
Page 206 and 207: SOUTH AFRICA’S NUCLEAR HYDROGEN P
Page 216 and 217: INTEGRATED LABORATORY SCALE DEMONST
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Page 229 and 230: RECENT CANADIAN ADVANCES IN THE THE
Page 237 and 238: AN OVERVIEW OF R&D ACTIVITIES FOR T
Page 245 and 246: STUDY OF THE HYDROLYSIS REACTION OF
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Page 262 and 263: EXERGY ANALYSIS OF THE Cu-Cl CYCLE
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EXERGY ANALYSIS OF THE Cu-Cl CYCLE
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CaBr 2 HYDROLYSIS FOR HBr PRODUCTIO
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SESSION V: ECONOMICS AND MARKET ANA
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DEVELOPMENT OF THE HYDROGEN ECONOMI
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NUCLEAR H 2 PRODUCTION - A UTILITY
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ALKALINE AND HIGH-TEMPERATURE ELECT
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THE PRODUCT OF HYDROGEN BY NUCLEAR
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SUSTAINABLE ELECTRICITY SUPPLY IN T
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PROHYTEC, THE FRENCH INDUSTRIAL PLA
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NHI ECONOMIC ANALYSIS OF CANDIDATE
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MARKET VIABILITY OF NUCLEAR HYDROGE
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POSSIBILITY OF ACTIVE CARBON RECYCL
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NUCLEAR SAFETY AND REGULATORY CONSI
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TRANSIENT MODELLING OF S-I CYCLE TH
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PROPOSED CHEMICAL PLANT INITIATED A
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CONCEPTUAL DESIGN OF THE HTTR-IS NU
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USE OF PSA FOR DESIGN OF EMERGENCY
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HEAT PUMP CYCLE BY HYDROGEN-ABSORBI
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HEAT EXCHANGER TEMPERATURE RESPONSE
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ALTERNATE VHTR/HTE INTERFACE FOR MI
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POSTER SESSION CONTRIBUTIONS Poster
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ACTIVITIES OF NUCLEAR RESEARCH INST
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ACTIVITIES OF NUCLEAR RESEARCH INST
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A URANIUM THERMOCHEMICAL CYCLE FOR
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A URANIUM THERMOCHEMICAL CYCLE FOR
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MEETING ORGANISATION Annex 1: Meeti
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LIST OF PARTICIPANTS REYTIER, Magal
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LIST OF PARTICIPANTS BROWN, Nichola
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LIST OF PARTICIPANTS SINK, Carl US
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